EP0367765B2 - Astaxantin liefernde hefezellen, verfahren zur herstellung - Google Patents

Astaxantin liefernde hefezellen, verfahren zur herstellung Download PDF

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Publication number
EP0367765B2
EP0367765B2 EP88903778A EP88903778A EP0367765B2 EP 0367765 B2 EP0367765 B2 EP 0367765B2 EP 88903778 A EP88903778 A EP 88903778A EP 88903778 A EP88903778 A EP 88903778A EP 0367765 B2 EP0367765 B2 EP 0367765B2
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yeast
astaxanthin
cells
dry matter
cell
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EP0367765A1 (de
EP0367765B1 (de
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Bent Fleno
Ib Christensen
Robert Larsen
Steffen Radich Johansen
Eric A. Johnson
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DSM IP Assets BV
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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
    • C12N1/14—Fungi; Culture media therefor
    • C12N1/16—Yeasts; Culture media therefor
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23D—EDIBLE OILS OR FATS, e.g. MARGARINES, SHORTENINGS, COOKING OILS
    • A23D7/00—Edible oil or fat compositions containing an aqueous phase, e.g. margarines
    • A23D7/005—Edible oil or fat compositions containing an aqueous phase, e.g. margarines characterised by ingredients other than fatty acid triglycerides
    • A23D7/0053—Compositions other than spreads
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23D—EDIBLE OILS OR FATS, e.g. MARGARINES, SHORTENINGS, COOKING OILS
    • A23D7/00—Edible oil or fat compositions containing an aqueous phase, e.g. margarines
    • A23D7/005—Edible oil or fat compositions containing an aqueous phase, e.g. margarines characterised by ingredients other than fatty acid triglycerides
    • A23D7/0056—Spread compositions
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J1/00—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites
    • A23J1/18—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from yeasts
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K20/00—Accessory food factors for animal feeding-stuffs
    • A23K20/10—Organic substances
    • A23K20/179—Colouring agents, e.g. pigmenting or dyeing agents
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K50/00—Feeding-stuffs specially adapted for particular animals
    • A23K50/80—Feeding-stuffs specially adapted for particular animals for aquatic animals, e.g. fish, crustaceans or molluscs
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L17/00—Food-from-the-sea products; Fish products; Fish meal; Fish-egg substitutes; Preparation or treatment thereof
    • A23L17/70—Comminuted, e.g. emulsified, fish products; Processed products therefrom such as pastes, reformed or compressed products
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L5/00—Preparation or treatment of foods or foodstuffs, in general; Food or foodstuffs obtained thereby; Materials therefor
    • A23L5/40—Colouring or decolouring of foods
    • A23L5/42—Addition of dyes or pigments, e.g. in combination with optical brighteners
    • A23L5/43—Addition of dyes or pigments, e.g. in combination with optical brighteners using naturally occurring organic dyes or pigments, their artificial duplicates or their derivatives
    • A23L5/44—Addition of dyes or pigments, e.g. in combination with optical brighteners using naturally occurring organic dyes or pigments, their artificial duplicates or their derivatives using carotenoids or xanthophylls
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L5/00—Preparation or treatment of foods or foodstuffs, in general; Food or foodstuffs obtained thereby; Materials therefor
    • A23L5/40—Colouring or decolouring of foods
    • A23L5/42—Addition of dyes or pigments, e.g. in combination with optical brighteners
    • A23L5/46—Addition of dyes or pigments, e.g. in combination with optical brighteners using dyes or pigments of microbial or algal origin
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
    • C12N1/14—Fungi; Culture media therefor
    • C12N1/145—Fungal isolates
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P23/00—Preparation of compounds containing a cyclohexene ring having an unsaturated side chain containing at least ten carbon atoms bound by conjugated double bonds, e.g. carotenes
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12R—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES C12C - C12Q, RELATING TO MICROORGANISMS
    • C12R2001/00—Microorganisms ; Processes using microorganisms
    • C12R2001/645—Fungi ; Processes using fungi
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
    • Y02A40/80—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in fisheries management
    • Y02A40/81—Aquaculture, e.g. of fish
    • Y02A40/818—Alternative feeds for fish, e.g. in aquacultures

Definitions

  • the present invention relates to astaxanthin-producing yeast strains, methods for their preparation, methods for their cultivation, and methods for isolating the astaxanthin from the yeast cells. Further, the invention relates to a food or feed which contains the astaxanthin-containing yeast cells or astaxanthin recovered from these as well as a method for producing food or feed and a method for feeding animals with said feed.
  • red colour of the meat of anadromous fish such as salmon or sea trout is due to red pigments such as astaxanthin which is present in the feed consumed by the fish.
  • red pigments such as astaxanthin which is present in the feed consumed by the fish.
  • the fish obtain their red colour from crustaceans or other astaxanthin-containing organisms, but when being bred in fish farms, the fish do not have access to these natural pigmentation sources and therefore do not obtain the attractive red colour unless red pigments are supplied in the feed.
  • astaxanthin isolated from crustacean wastes or produced synthetically as well as other synthetic red pigments such as cantaxanthin have been used as constituents in fish feed.
  • cantaxanthin in animal feedstuffs is prohibited in certain countries, and the synthetic astaxanthin production as well as the process for isolating natural astaxanthin are rather expensive and often also subject to seasonal variations.
  • yeast Phaffia rhodozyma and some microalgae such as the unicellular group of green algae Chlamydomonas nivalis [Gert Knutson et al., "Pigmentering at laks med astaxanthin fra mikroalger", Norsk Fiskeopdr ⁇ t nr. 3, pp. 4-6, 55 (1980)].
  • the astaxanthin produced by these organisms has been shown to confer the desired red colour to anadromous fish [Eric A. Johnson et al., " Phaffia rhodozyma as an astaxanthin source in salmonid diets", Aquaculture, 20, pp.
  • yeast cells in large amounts as nutrition for the fish is not desirable as this feed is not sufficiently varied.
  • the amount of astaxanthin produced by the organisms and present in a nutritionally acceptable amount of yeast cells is not sufficient to obtain the desired pigmentation, and the isolation of astaxanthin from yeast by the known methods is rather expensive.
  • the present invention provides Phaffia rhodozyma yeast cells which contain astaxanthin in sufficiently high concentrations to make it possible to use the yeast cells as or in feed for anadromous fish and other animals in which a pigmentation of the animal meat or a product of the animal is desired.
  • the invention also provides attractive methods for obtaining astaxanthin from astaxanthin-containing yeast cells, in particular the above-mentioned yeast cells having high contents of astaxanthin.
  • Important aspects of the invention are based on a particular method for cultivating astaxanthin-producing cells and/or the provision of mutant strains with an improved inherent capability of producing astaxanthin.
  • one aspect of the invention relates to a Phaffia rhodozyma yeast cell which, is a yeast cell belonging to the yeast strain deposited under the accession No. 225-87 CBS, or the yeast strain deposited under the accession No. 215-88 CBS, or a mutant or derivative thereof, or a mutant or derivative of the yeast strain deposited under the accession No.
  • 173-83 are based on the absorbance of a 1% (w/v) solution in acetone in a 1 cm cuvette of 1600, whereas the value, which is obtained by measuring the astaxanthin standard from Hoffmann-La Roche, is 2100. This value is based on the applicant company's own measurements as well as on the information given by Hoffmann-La Roche.
  • the known determination method measures the total pigment content of the yeast whereas the above-mentioned standard method used in the present application exclusively measures the astaxanthin content.
  • the values stated in the literature will be considerably higher than the true values obtained by the standardized method stated above.
  • a correction for the difference in extinction coefficients should be made by multiplying the total pigment content stated in the literature by 1600/2100.
  • the yeast cell according to the invention is one which belongs to the species Phaffia rhodozyma as this is the only Phaffia species known for the time being.
  • Phaffia rhodozyma is the only known yeast which produces astaxanthin.
  • the wild-type P. rhodozyma is isolated from deciduous tree exudates and an example of such a wild-type strain is deposited in the American Type Culture Collection under the accession number ATCC 24261.
  • Vegetative P. rhodozyma cells form buds as heterobasidiomycetous yeast. Clamydospores are developed by budding but promycelium and proper spore formation do not occur. The chlamydospores are relatively large spherical cells with a larger lipid content than the vegetative cells. Attempts to pair the various strains in the hope of observing dikaryotic mycelium and teliospore formation have not been successful. P. rhodozyma was therefore classified in the genus Deuteromycotina of the order Blascomycetes (cf. M.W. Miller et al., "Phaffia, a new yeast genus in the deuteromycotina (Blastomycetes)-", in International Journal of systematic bacteriology 26:2, 1976, pp. 286-291).
  • Vegetative cells are ellipsoidal (3.6-7.5) x (5.5-10.5) ⁇ m and are present in a liquid medium individually, in pairs and in some cases in short chains or small clusters. No true mycelium is developed, but a rudimentary pseudomycelium may be present. Budding occurs several times from the same point on the cell.
  • P. rhodozyma has a strong cell membrane composed by many layers, and capsule material imparts a granular appearance to the surface and causes the clustering mentioned above.
  • a sexual cycle of life has not been observed.
  • vegetative cells are formed by budding. These cells cannot be considered to be promycelia with spores as described for Aessosporon (cf. J.P. van der Walt, "The perfect and imperfect states of Sporobolomyces salminicolor", J. Microbiol. Serol. 36 , 1970, pp. 49-55).
  • the chlamydospores cannot be considered to be gonotoconter (sexually segregated spores), and their buds cannot be considered to be the haploid generation. It has not been possible by nuclear staining to demonstrate diploidization at any growth stage.
  • P. rhodozyma has the special property of not growing at temperatures above 27 °C. It ferments D-glucose, maltose, sucrose and raffinose whereas D-galactose and melibiose are not fermented.
  • the most common carbon sources are assimilated; however, D-galactose, L-sorbose, melibiose, lactose, glycerol and citrate are not assimilated.
  • the yeast cannot grow in vitamin-free medium without the addition of biotin (M.W. Miller et al., op.cit .).
  • the most common nitrogen sources are assimilated, including urea.
  • Potassium nitrate and ethylamine are not assimilated.
  • the yeast cannot grow on 50% by weight of a glucose-yeast extract agar nor on 10% by weight of sodium chloride-yeast extract agar.
  • the acid formation on chalk agar by the yeast is weak and so is the gelatin liquefaction.
  • Casein hydrolysis, depolytic activity and growth in the presence of 0.1 ⁇ g of cycloheximid per ml are absent whereas the yeast is able to synthesize starch-like compounds independent of pH.
  • the mole-% G + C is measured to be 48.3 ⁇ 0.18 (cf. Miller et al., op. cit .).
  • P. rhodozyma produces a number of carotenoids, of which astaxanthin constitutes 83-87%, ⁇ -carotene 2-2.5%, echinenone 2-4% and phoenicoxanthin 5-7%, according to the literature.
  • the ratio of astaxanthin to total pigment produced by P. rhodozyma has, however, been found to vary considerably depending on the growth conditions of the yeast cells as well as the pigment determination method and has generally been found to be in the range of 50-80%. All hydroxylated pigments, including astaxanthin, have been described as non-bound, not as esters or other derivatives (Arthur G.
  • the pigment in the individual P. rhodozyma cells is not visible when the cells are studied in a microscope, which indicates that the pigment may be dispersed throughout the cell. However, it is also possible that the pigment is concentrated in certain parts of the cells.
  • Astaxanthin is an oxidated carotenoid and therefore belongs to the xanthophyl group. Similarly to other carotenoids, astaxanthin is composed of eight isoprenoid units.
  • isopentenyl pyrophosphate is formed from acetyl-CoA as illustrated below.
  • isopentenyl pyrophosphate forms geranyl geranyl pyrophosphate via geranyl pyrophosphate and farnesyl pyrophosphate as illustrated below.
  • rhodozyma produces (3R,3'R)-astaxanthin and whether there are some regulating steps during this part of the biosynthesis.
  • the conversion of acetyl-CoA to isopentenyl pyrophosphate in other isoprenoid-producing organisms than P. rhodozyma and the enzymes which take part have been described in relatively great detail. Less is known about the enzymes which convert isopentenyl pyrophosphate to geranyl geranyl pyrophosphate (isopentenyl pyrophosphate isomerase and prenyltransferase (J.W. Porter, S.L. Spurgeon (eds.), "Biosynthesis of isoprenoid compounds”. New York, 1981-1983).
  • the protein content of P. rhodozyma varies from 25 to 50% of yeast dry matter, depending on the culturing conditions. This is a relatively low protein content. In contrast to this, the lipid content is extraordinarily high (14-27%). It is contemplated that the nucleic acid constitutes 8% similarly to other yeasts and that the amino acid composition is similar to the composition in other known yeasts such as Saccharomyces cerevisiae and thus has a very low content of certain amino acids, e.g. methionin and cystein (cf. Gerald Reed and Henry J. Peppler, Yeast Technology , 1973, p 329, published by The AVI Publishing Company, Inc.).
  • yeast This and the overall yeast composition which comprises a high amount of nucleic acids make the yeast inconvenient for animal nutrition purposes when the yeast is the only nutrient source, such as indicated above. Thus, without addition of certain amino acids and other nutrient components, the yeast will not be a suitable major nutrition component for fish or other animals.
  • the total amount of astaxanthin which is produced by the wild type P . rhodozyma when this is grown under the normal known conditions is sufficient to confer a red colour to the yeast cell but is not sufficient to make recovery of the astaxanthin from the yeast cells economically feasible.
  • the present invention discloses a method for producing a yeast cell showing the high inherent astaxanthin-producing capability explained above, the method comprising treating a yeast cell with a mutagen and selecting a resulting mutant which, when grown under the conditions stated above, is capable of producing astaxanthin in an amount of at least 600 ⁇ g per g of yeast dry matter, determined by the method stated above.
  • the mutagenization may be performed as a single mutagenization, but it has been found advantageous to perform two or more consecutive mutagenizations, as it has been found that the inherent capability of producing astaxanthin may be improved by each mutagenization step.
  • the starting yeast cell subjected to mutagenization is normally a yeast cell which, when grown under the conditions stated above, produces astaxanthin in an amount of less than 300 u.g per g of yeast dry matter, determined by the method stated above, but it is evident that a normal candidate for the mutagenization treatment will be a naturally occurring yeast cell having as high inherent astaxanthin production as possible.
  • yeast cells are normally yeast cells which belong to the genus Phaffia , in particular yeast cells belonging to the species Phaffia rhodozyma , such as is mentioned above.
  • the mutagenization treatment may be performed using any suitable mutagen (in the present context, the term "mutagen” is to be understood in its broad sense as comprising, e.g., not only agents which have a mutagen effect, but also treatment which have a mutagen effect such as UV irradiation).
  • suitable mutagens are ethyl methane sulphonate, UV irradiation, N-methyl-N'-nitro-N-nitrosoguanidine, nucleotide base analogues such as bromouracil, and acridines, but it is contemplated that any other effective mutagen will be suitable for the treatment.
  • the mutagenization is followed by suitable selection of the cells which have the highest astaxanthin production. Due to the fact that astaxanthin is a pigment, this selection may be performed relatively easily by normal visual means, such as simple observation of single colonies.
  • An alternative method is to perform analysis on cultures made from single colonies, e.g. by using the standardized cultivation conditions and determination conditions as explained above.
  • the invention also relates to a method for producing astaxanthin-containing Phaffia rhodozyma yeast cells according to Claim 1 or cell parts, or astaxanthin derived from these yeast cell or cell parts.
  • This method comprises cultivating astaxanthin-producing yeast cells under aerobic conditions in a medium containing carbohydrate sources, assimilable sources of nitrogen and phosphorus, micronutrients and biotin or desthiobiotin at a temperature in the range of 15-26°C so as to obtain a biomass containing astaxanthin in an amount of at least 600 ⁇ g per g of yeast dry matter, determined by the method stated above, and optionally performing one or several of the following steps in arbitrary sequence:
  • the amount of astaxanthin stated above, 600 u.g per g of yeast dry matter, is higher than any astaxanthin concentration reported in the literature.
  • Johnson et al., op. cit . reports an astaxanthin content of up to 814 ⁇ g per g of yeast dry matter, this value does not only comprise the astaxanthin content but in fact the total pigment content of the yeast cell. Further, this pigment content was measured using a value of the absorbance of a 1% (w/v) solution in acetone in 1 cm cuvette of 1600 which is lower than the one measured by the present applicants (2100) so that the value reported by Johnson et al.
  • the value of Johnson et al. corresponds to at most 540 ⁇ g of astraxanthin per g of yeast dry matter.
  • This pigment content from the literature should be compared with the total pigment content of the yeast strains of the present invention which is 885 ⁇ g/g of yeast dry matter for the strain CBS 224-87, 1176 ⁇ g/g of yeast dry matter for the strain CBS 225-87, and about 1340 ⁇ g/g of yeast dry matter for the strain CBS 215-88, or even higher.
  • the high astaxanthin concentration in the yeast cells of the invention may be obtained partly by the use of special cultivation conditions as explained below and partly by selecting a yeast strain with a high inherent astaxanthin productivity, preferably a yeast strain as discussed above, and in particular it is preferred to combine the special cultivation conditions and the use of special astaxanthin-producing yeast strains.
  • the cultivation is preferably performed as a fed-batch fermentation under conditions where substantially no alcohol is formed.
  • the temperature of the culture is in the range of 15-26°C. Below 15°C, the growth tends to be too slow to be acceptable for industrial production, and above 26°C, the viability of the culture is severely impaired.
  • the preferred temperature range is 20-22°C.
  • the fermentation or at least part thereof is normally performed in a medium which comprises suitable macro- and micronutrients for the cells, such as molasses or saccharose as a carbohydrate source and nitrogen sources such as corn-steep-liquor, diammonium sulphate, ammonium phosphate, ammonium hydroxide or urea, phosphorus sources such as ammonium phosphate and phosphoric acid and added micronutrients or mineral salts such as magnesium sulphate, zinc sulphate and biotin or desthiobiotin.
  • suitable macro- and micronutrients for the cells such as molasses or saccharose as a carbohydrate source and nitrogen sources such as corn-steep-liquor, diammonium sulphate, ammonium phosphate, ammonium hydroxide or urea, phosphorus sources such as ammonium phosphate and phosphoric acid and added micronutrients or mineral salts such as magnesium sulphate, zinc sulphate and
  • the medium comprises molasses
  • the concentration of sugar (expressed as the total concentration of glucose and saccharose) in the fermenter is at the most 8 g/l, preferably at the most 5 g/l, and most preferably at the most 1 g/l.
  • the culture is aerated during the total fermentation, i.e. it is grown under aerobic conditions.
  • aerobic conditions is meant that the oxygen supply should be sufficient so that substantially no oxygen limitation will occur during the fermentation.
  • the concentration of astaxanthin in the biomass obtained is increased by performing the cultivation under selected conditions.
  • These conditions involve a cultivation which comprises a growth phase under conditions which are substantially sufficient with respect to substantially all growth conditions and a subsequent growth-limited phase.
  • the growth-limited phase is preferably established by providing conditions where the growth medium under continued aeration is deprived of at least one growth factor so as to enhance the production of astaxanthin during the subsequent phase.
  • the growth-limited phase should be understood to generally mean the phase in which the main part of the cells have stopped growing. This phase does of course occur when the medium is deprived of at least one growth factor but is also observed during the last part of the period of carbohydrate addition when the amount of cells present in the fermenter is well in excess of the aeration capacity of the fermenter.
  • the subsequent growth-limited phase has the surprising effect of considerably enhancing the production of astaxanthin (for example from 231 to 369 ⁇ g per g of yeast dry matter as obtained in one of the examples which follows), but it is contemplated that the precursors of astaxanthin have been produced during the growth phase, and that the subsequent growth-limited phase provides conditions which promote the final production of astaxanthin, possibly oxidizing conditions with the surplus of oxygen which becomes available when the growth is terminated. At any rate, it seems essential that aeration is continued during the subsequent growth-limited phase.
  • the duration of the subsequent growth-limited phase is preferably at least about 16 hours, such as 16-24 hours, as shorter durations may tend to decrease the extra effect obtainable, whereas there seems to be no substantial effect obtainable by extending the growth-limited phase to more than about 24 hours.
  • the conditions of the growth-limited phase should be adapted to enhance the astaxanthin production to at least 1.2 times the production obtained without the subsequent phase, such as at least 1.3 times the production obtained without the subsequent phase, preferably at least 1.4 times the production obtained without the subsequent phase and most preferably at least 1.5 times the production obtained without the subsequent phase.
  • the yeast cell subjected to the special cultivation with the subsequent growth-limited phase is a yeast cell according to the invention having an inherent and improved capability of producing astaxanthin, typically a yeast cell obtained by mutagenization as explained above.
  • the concentration of astaxanthin in the biomass obtained when using the special cultivation method comprising a growth-limited phase may be at least 600, preferably at least 800, more preferably at least 1000 ⁇ g per g of yeast dry matter, determined as stated above.
  • the total pigment content and astaxanthin content of the yeast cells or yeast cell parts are stated as ⁇ g/g of yeast dry matter.
  • other ways of stating the total pigment and astaxanthin content may be found convenient. It may, e.g., be useful to state the total pigment content and astaxanthin content as ⁇ g/ml of the suspension in which it is present, e.g. in the growth media. Thereby, it will not be necessary to determine the weight of yeast dry matter of the yeast cells from which the astaxanthin or total pigment is recovered. Thus, during the fermentation or cultivation of the yeast cells, the astaxanthin and/or total pigment content of the yeast cells may easily be determined.
  • the culture may be subjected to the subsequent treatments mentioned above to isolate the yeast cells and/or condition them for their subsequent use, such as by rupturing the cells, and/or astaxanthin may be extracted from the cells.
  • the cells may be ruptured by subjecting the cells to an increased pressure and then releasing the pressure.
  • the cells may be subjected to the increased pressure and release of the pressure by passage through a system comprising a valve homogenizer where the increased pressure is built up in front of the valve homogenizer.
  • the valve homogenizer typically comprises an aerojet through which the cell suspension is passed under high pressure and an obstruction member which the jet hits substantially after passage through the valve. Examples of cell disruption valves are described in APV Gaulin Technical Bulletin No. 74 of March 1985 (APV Gaulin International SA, P.O. Box 58, 1200 AB Hilversum, the Netherlands), incorporated by reference herein.
  • a suitable cell rupture homogenizer may be mentioned an APV Gaulin MC4 homogenizer with a cell rupture valve of the type CR as described in the above-mentioned publication.
  • the homogenizer is connected to a a heat exchanger in which the suspension comprising ruptured cells passes from the cell rupture valve.
  • the pressure of the cell suspension in front of the valve may, e.g., be about 400-1200 bar, such as, e.g., about 700 bar. This treatment may for example be repeated three times with intervening cooling of the homogenate in the heat exchanger.
  • the ruptured yeast cells may be subjected to ultrafiltration or evaporation so as to concentrate the ruptured cells.
  • the ultrafiltration may, e.g., be performed in a lab unit system available from De Danske Sukkerfabrikker, for example a System 37 which comprises three filtering units of a total filter area of 0.88 m 2 of an ultrafiltration membrane of the type RC 70.
  • Another method for concentrating the ruptured cells is to perform vacuum evaporation of water from the cell suspension.
  • the ruptured cells may be dried by spray drying or drum drying. Before drying, carriers such as sodium caseinate, antioxidants and/or emulsifiers are preferably added.
  • Spray drying may, e.g., be performed by subjecting a homogeneously mixed slurry of the ruptured cells and optionally a carrier such as sodium caseinate, preferably in the form of an aqueous solution, to spray drying.
  • the spray drying may suitably be carried out by mixing the aqueous sodium caseinate solution with the yeast slurry so as to obtain a sodium caseinate concentration of about 2-10% (w/v).
  • the resulting mixture is then allowed to stand with stirring in a nitrogen atmosphere before being pumped into a spray drying tower in which it is subjected to drying at a temperature of, e.g., 150-230°C, such as about 180°C to decrease the water content of the yeast cell material to e.g. at the most 10% by weight.
  • the yeast cell material is then subsequently atomized by means of a spray wheel.
  • the powdery yeast material resulting from the spray drying treatment is suitably recovered by means of cyclone and optionally subsequently sieved and packed.
  • An example of a suitable spray drying equipment is a spray tower of the type EAK-1 from Anhydro.
  • the ruptured yeast cells may be subjected to drum drying, for example in a closed drum drying equipment at a temperature of 150-200 °C.
  • the drying should preferably be performed under non-oxidizing conditions, for example in an inert atmosphere such as water vapour (which may be the water vapour evaporated from the yeast suspension), nitrogen, and/or carbon dioxide.
  • the ruptured cells Prior to drying, the ruptured cells are optionally mixed with suitable emulsifiers such as sorbitan monostearate or antioxidants, butyl hydroxytoluene (BHT), butyl hydroxyanisol (BHA), vitamin E, ascorbic acid, (II) sulphate or (II) phosphate esters of ascorbic acid, or ascorbyl palmitate.
  • suitable emulsifiers such as sorbitan monostearate or antioxidants, butyl hydroxytoluene (BHT), butyl hydroxyanisol (BHA), vitamin E, ascorbic acid, (II) sulphate or (II) phosphate esters of ascorbic acid, or ascorbyl palmitate.
  • Dried ruptured cells are immediately useful as a constituent of animal feed, such as is explained below.
  • the astaxanthin content of the yeast cell may be extracted from these by use of various extraction agents and extraction procedures - so as to ensure that a substantial total extraction of the astaxanthin from the yeast cells is obtained.
  • the extraction has to be performed in ruptured cell material.
  • the ruptured cell material which may be dry or wet, may be extracted with an organic solvent such as petroleum ether which is suitably employed in the case of wet cell material as the petroleum ether forms a phase separately from the water phase.
  • suitable organic solvents are acetone or alcohols such as methanol or ethanol, ethers, ketones and chlorinated hydrocarbons.
  • the astaxanthin may be obtained by removing the solvent from the solution such as by evaporation in a falling film evaporation system before drying.
  • a concentrate of astaxanthin in the organic solvent may be convenient for certain purposes.
  • a concentrate may be used per se in the production of feed or food, or the concentrate may be diluted and used in the diluted state in the preparation of feed or food, for example by impregnating feed or food constituents with the solution or by using the solution (or the concentrate) for colouring food constituents such as oils or fats.
  • the astaxanthin may also be extracted from yeast cells by use of carbondioxides under supercritical conditions.
  • the carbondioxide may optionally be used in combination with suitable entrainers such as organic solvents, especially solvents of the above mentioned types, or solvents such as chloroform or acetonitrile, or glacial acetic acid.
  • suitable entrainers such as organic solvents, especially solvents of the above mentioned types, or solvents such as chloroform or acetonitrile, or glacial acetic acid.
  • suitable entrainers such as organic solvents, especially solvents of the above mentioned types, or solvents such as chloroform or acetonitrile, or glacial acetic acid.
  • the yeast cells subjected to supercritical extraction may be wet or dry whole yeast cells or ruptured, e.g. homogenized, yeast cells.
  • a preferred method of isolating whole astaxanthin-containing cells from the culture is to filtrate the yeast cream, for example on a filter press or a rotating drum filter, so as to obtain a filter cake, e.g. with a dry matter content of about 25-35%.
  • the filter cake may then suitably be extruded into strings, for example strings with a diameter of about 0.5-2.0 mm in an extruder equipped with a perforated plate, so as to obtain strings consisting of yeast particles.
  • the strings are preferably extruded directly into the hot air in a fluid bed where they are dried.
  • the evaporation in the fluid bed is preferably regulated so that the temperature of the yeast particles is kept below 50°C such as at 30-40°C, and the process is terminated when the water content is brought down below 10% by weight, preferably below 8%, as determined by the yeast dry matter content (the procedure is described in the Examples).
  • the drying may be performed in a tray drier under the same conditions as in the fluid bed.
  • the dried whole cell material may then be comminuted in a ball stirring mill such as a Coball® mill after which it is subjected to extraction.
  • whole cell dried material for example obtained as described above, may be mixed with an oily phase such as an edible oil or fat such as soy bean oil or fish oil, or another organic solvent such as a solvent of the type discussed above.
  • the temperature is preferably in the range of 20-30°C.
  • the mixture obtained from the cell material and the oily phase or the organic solvent may be ground in a mill such as a ball mill, e.g. a ball stirring mill such as a Coball® mill, to rupture the cells and release astaxanthin from the cells.
  • the resulting suspension may be used as such in feed, or the oily phase containing the astaxanthin may be separated from cell residues before use. The separation is suitably performed by centrifugation in a fast running centrifuge.
  • astaxanthin may be extracted from whole yeast cells with a solvent comprising glacial acetic acid, the extraction preferably being performed at a temperature above the freezing point of the solvent, e.g. in the range of 20-100°C, preferably in the range of 20-80°C, and more preferably in the range of 20-60°C.
  • the concentration of glacial acetic acid in the solvent is preferably in the range of 5-100, 10-70.
  • the extraction with glacial acetic acid results in an extraction of the pigment of the cells of about 70-90%, i.e. substantially all the pigment and astaxanthin contents of the yeast cells are found in the glacial acetic acid extract.
  • the extract normally contains about 30-35% of yeast dry matter.
  • the yeast subjected to extraction with glacial acetic acid is in the form of dried yeast, e.g.
  • yeast which has been filtered and subsequently extruded into a fluid bed wherein it is dried, as thus treated yeast cells will not rupture during the extraction treatment (unless the extraction treatment involves vigorous mechanical treatment of the yeast cells). This will facilitate the subsequent separation of the extract containing the pigment from the yeast cells as compared with extraction of ruptured or homogenized cells, which, due to their relatively small sizes in comparison with non-ruptured cells to a large extend tend to block up the pores of the filter employed.
  • the glacial acetic acid extraction is illustrated in Example 9. Extraction of wet yeast cells with glacial acetic acid may also prove useful.
  • the extracted astaxanthin as well as the whole dried cell material are preferably kept under oxygen-deficient conditions so as to protect the astaxanthin from decomposition.
  • the astaxanthin-containing yeast cells or the extracted astaxanthin is preferably protected by means of antioxidants such as butyl hydroxyanisol (BHA). butyl hydroxytoluene (BHT), vitamin E or ascorbic acid, (II) sulphate or (II) phosphate esters of ascorbic acid, or ascorbyl palmitate, and or emulsifiers such as monoglycerides or sorbitan esters and are suitably kept under hermetic conditions.
  • the yeast cells according to Claim 1 or yeast cell parts containing astaxanthin in an amount of at least 600 ⁇ g per g of yeast dry matter, determined as explained above are useful for animal feed, in combination with other feed constituents.
  • the astaxanthin-containing yeast cells or yeast cell parts constitute at the most 10% by weight of the dry matter of the total animal feed composition, preferably at the most 5% and more preferably at the most 3%. These values are calculated on the final feed to be administered to the animals. It is also possible to prepare feed premixes having a higher concentration of yeast cells.
  • the yeast cells or yeast cell parts or the astaxanthin is optionally admixed with emulsifiers which are capable of making the astaxanthin dispersible in water.
  • the astaxanthin-containing yeast cells or yeast cell parts may be protected against oxidation by means of the antioxidants and or emulsifiers mentioned above, and/or the animal feed may be packaged in air-tight and optionally evacuated containers.
  • the astaxanthin-containing dried yeast cells may also be packaged per se for use as a feed constituent, the final feed mixture being prepared at the site of use. or the yeast cells being administered per se to animals which are otherwise fed with normal or adapted feed mixtures
  • the yeast cells or yeast cell parts are suitably and normally mixed with other nutrient components which are preferably selected from protein and carbohydrate sources, fats or oils and micronutrients such as vitamins and minerals.
  • protein sources may be mentioned casein, albumin, wheat gluten, fish meals. concentrated fish residues (fish glue meal and blood meal).
  • carbohydrate sources may be mentioned gelatinized starch, extruded wheat, molasses, vegetable flours and corn starch.
  • the fat constituents in the feed may for example be fish oil and cod liver oil and or vegetable oils such as corn oil.
  • the minerals may be selected, e.g., from inorganic or simple organic compounds of calcium, phosphorus, sodium, potassium, chlorine, magnesium, copper, manganese, zink, cobalt and selenium.
  • vitamins may be mentioned vitamin B 12 , proline, vitamin A, vitamin D, vitamin E, vitamin K, thiamine, ascorbic acid, riboflavin, pyridoxin, panthotenic acid, niacin, biotin, choline and inositol.
  • the invention also makes it possible to provide food or feed comprising astaxanthin which has been extracted from Phaffia rhodozyma yeast cells, for example by any of the methods described above, preferably from yeast cells according to the invention or yeast cells produced by the method of the invention.
  • the astaxanthin may be used in admixture with the feed constituents described above and also in admixture with other food or nutrient components as well as in admixture with other colourants.
  • astaxanthin extracted from yeast cells is well suited alone or in combination with other colourants for use in edible oils, butter, margarine, shortening, mayonnaise, patés, soups, snack products, surimi-based products, desserts, ice cream, confectionery. baked products, and beverages.
  • the astaxanthin When the astaxanthin is used in food which is mostly constituted by water or water phases, the astaxanthin is preferably mixed with an emulsifier as discussed above which makes the astaxanthin dispersible in the water phase without any tendency to crystallize and without the necessity of adding an oily phase to dissolve the astaxanthin.
  • the invention according to claim 1 relates to a method for feeding animals to obtain a reddish pigmentation of their meat and or of products produced by the animals, comprising administering to the animals a feed containing Phaffia rhodozyma yeast cells according to Claim 1 or cell parts containing astaxanthin in an amount of at least 600 ⁇ g per g of yeast dry matter, determined by the method stated above, or astaxanthin extracted from such yeast cells or cell parts.
  • the amount of the feed containing the astaxanthin or the astaxanthin-containing yeast cells or cell parts administered to the animals will depend upon the animal species in question and upon the pigmentation effect which it is desired to obtain by means of the astaxanthin.
  • the principle to be followed is that the animal should have a normal recommended daily ration of macro- and micronutrients and, in addition, astaxanthin in a form and an amount which will result in the desired pigmentation of the animal meat or the animal product in question.
  • the amount of astaxanthin to be administered will depend on the season: thus, for example, it will normally not be preferred to administer astaxanthin or other carotenoids to cows to obtain a pigmentation of the butter in the summertime as the butter pigmentation is normally considered adequate when the cows are grazing.
  • the amount in which the feed containing the astaxanthin or the astaxanthin-containing yeast cells or cell parts is administered to the animals may in some cases be dependent on the season.
  • the amount of feed consumed by the fish in the wintertime is relatively low which is in contrast to the amount consumed by the fish in the summertime.
  • a suitable amount of feed administered to the fish may be about 1.5% of fish body weight per day which corresponds to the recommendations given by the California State Department of Fish and Game.
  • the feed When feeding poultry by the method stated above in order to pigment the yolks of the eggs produced by the poultry and/or the meat or skin of the poultry, the feed may be constituted by conventional poultry feed components.
  • an example of which is one which is preferably constituted by protein and carbohydrate sources such as soy bean meal, soy bean protein, cellulose, starch and fat sources such as soy bean oil, vitamins such as an overall vitamin mix and minerals such as a mixture of the common mineral components for poultry as well as calcium sources for the egg shells, the calcium sources preferably being calcium carbonate and calcium hydrogen phosphate.
  • a small amount of sodium chloride may also be present.
  • the feed may be administered in a conventional dosage.
  • YDMC yeast dry matter content
  • the total pigment content in a methanol extract is determined spectrophotometrically by means of ⁇ max and Beer's law as described by B.H. Davies, "Carotenoids", in T.W. Goodwin (ed.), Chemistry and Biochemistry of plant pigments, New York, 1976, Vol. 2, p. 149.
  • the spectrophotometer employed is a Shimadzu UV visible recording spectrophotometer UV 260. Pigment content is calculated by using formulas 1, 1a, 2, 2a below and the extinction coefficients of Table 1 below.
  • yeast culture About 30 ml of the yeast culture were transferred to Sarsteds tubes and centrifuged for 5 minutes at 10,000 x g.
  • the yeast cells were washed in demineralized water and suspended in about 20 ml of methanol.
  • a glass ball mill of the type Bead Beater Biospec Products Inc., USA
  • the rotor was covered with glass balls with a diameter of 0.4 mm (about 15 g of glass balls)
  • the methanol suspension was added so as to occupy the remaining free ball mill volume.
  • Disintegration treatment was carried out by running the mill 5 times for 1 minute at intervals of 30 seconds, ice water being kept in the cooling jacket so as to ensure that the temperature of the disintegration treatment was kept below 20°C.
  • a predetermined amount of the yeast culture (a ml) were transferred to Sarsteds tubes and centrifuged for 5 minutes at 10,000 x g.
  • the yeast cells were washed in demineralized water and suspended in about 20 ml of methanol.
  • a glass ball mill of the type Bead Beater Biospec Products Inc., USA
  • the rotor was covered with glass balls with a diameter of 0.4 mm (about 15 g of glass balls)
  • the methanol suspension was added so as to occupy the remaining free ball mill volume.
  • Disintegration treatment was carried out by running the mill 5 times for 1 minute at intervals of 30 seconds, ice water being kept in the cooling jacket so as to ensure that the temperature of the disintegration treatment was kept below 20°C.
  • the liquid was transferred to a 50 ml measuring flask.
  • the glass beads are washed in the mill with 4 x 8 ml of methanol.
  • the fractions are collected and mixed and methanol is added to give 50 ml.
  • the methanol extract is filtered before pigment analysis.
  • the yeast dry matter in the culture is determined as described above.
  • Standard solution 5 mg of pure astaxanthin (mp 220-222°C, absorbance of 1% v/w acetone solution in a 1 cm cuvette 2100) supplied by Hoffmann-La Roche (hereinafter referred to as the astaxanthin standard) are weighed out and dissolved in 500 ml of acetone.
  • Standard solution 5 mg of astaxanthin standard are weighed out and dissolved in 500 ml tetrahydrofurane.
  • Polypropylene centrifuge tubes provided with a polypropylene stopper of the type 55533 supplied by Hounisens Laboratory, ⁇ rhus, Denmark.
  • Chemicals used in a laboratory scale were of analytical grade. Chemicals used in fermentations were of food grade.
  • the glucose and saccharose concentrations were analyzed by of use of kits (Best. No. 139041) from Boehringer Mannheim.
  • YM(Yeast Morphology) medium supplied by Difco Laboratories Incorporated (Difco Manual: Dehydrated culture media and reagents for microbiology, 10th edition, Detroit, 1984).
  • the mutagenization treatment was carried out so as to obtain a degree of survival of 1-5% of the treated culture. Suitable mutants were selected by visually comparing the intensity of the red colour of the mutants when plated as single colonies on the agar plates.
  • a just turbid four days old culture of ATCC 24261 grown in YM medium at 20-22°C was diluted in a 0.9% NaCl solution to concentrations of 10 -1 , 10 -15 , 10 -2 , 10 -2.5 and 10 -3 , respectively, and 0.3 ml of each of these dilutions was plated on agar plates so as to obtain agar plates containing 100-300 colonies.
  • the plates were then subjected to ultraviolet irradiation at 254 nm for 30 seconds at a distance of 20 cm from the irradiation source (Vilbert Lourmat VL 30 LC) and then grown at 20-22 °C for 10 days after which the colour of the resulting colonies was compared.
  • the yeast cell suspension was then diluted and placed on agar plates in the same manner as described above for the UV-treatment.
  • One of the isolated mutants was deposited at the CBS (Centraalbureau voor Schimmelcultures) on 6 April, 1987 under the accession No. 224-87.
  • N-methyl-N'-nitro-N-nitrosoguanidine (Aldrich Chemie BDR) were added to a 10 ml cared graduated cylinder supplied with a glass stopper. Water was supplied so as to obtain a total volume of 10 ml, and the N-methyl-N'-nitro-N-nitrosoguanidine was dissolved therein by shaking. 10x1 ml of stock solution were obtained from this solution.
  • CBS 225-87 has been subjected to isolation as described as follows. From a freeze-dried vial yeast cells are suspended in YM medium and incubated for 5 day at 20-22°C. The culture is plated on YM plates and incubated for 10 days at 20-22°C and new colonies are isolated. One of the colonies is deposited at the CBS on 23 March, 1988 under the accession No. 215-88.
  • the yeast cell cultivation and the astaxanthin determination described in the present Example constitute, on the one hand, the conditions under which the yeast cells are grown and on the other hand the conditions under which astaxanthin is determined in the applicant's above-mentioned standard method for determining the inherent astaxanthin-producing capability of a yeast strain. These are the same standard conditions as are referred to in the claims.
  • 100 ⁇ l of a 4 days old culture of ATCC 24261 grown in YM medium on a shake board at 20-22 °C were inoculated in 50 ml of YM medium contained in a 500 ml shake flask with 2 baffles.
  • the culture was subjected to growth on a shake board with orbital shaking at 150 rpm for 5 days at 20-22 °C and at an oxygen transfer rate of 30 mmoles/l/hour, whereby a density of the yeast cell culture of 0.6% was obtained.
  • the astaxanthin content in the extract was identified by the following three methods.
  • the mutant strains of the invention (CBS 224-87 and CBS 225-87) as well as all known deposited astaxanthin-producing P. rhozodyma strains were grown and analyzed in the same manner as described above.
  • the total pigment content and the astaxanthin content of the strains are stated in Table 2 below.
  • mutant strains of the invention show a considerably increased astaxanthin content.
  • the fermentations were performed as fed-batch fermentations under carbohydrate limitation in thoroughly washed and sterilized 4 m 3 fermenters of the type Bubble Column with a stationary aeration system consisting of perforated air pipes.
  • the fermenters were equipped with pH electrodes, inlets for pH regulating agents and foam-suppressing agents, and alcohol detectors for measuring alcohol in the discharged air.
  • the jackets of the fermenters were thermostated.
  • the start wort has the following composition: 20 g/l of molasses, 0.6 g/l of diammonium sulphate, 0.8 g/l of diammonium hydrogenphosphate and 0.125 g/l of magnesium sulphate which altogether were boiled up in the fermenter for 30 minutes together with a suitable amount of water (30 I in the 100 I propagation fermenter and 2000 I in the 4 m 3 production fermenter) before the fermenter in question was inoculated.
  • the medium which was fed to the fermenter in the fed-batch fermentation was taken from two different reservoirs, i.e.
  • a chemical reservoir consisting of 10 kg of diammonium sulphate, 5.6 kg of diammonium hydrogenphosphate and 80 l of water; and a molasses reservoir consisting of 450 kg of molasses and 1000 I of water which had been autoclaved.
  • 0.1 mg of desthiobiotin and 1.6 kg of magnesium sulphate were supplied directly to the fermenter before the rest of the medium was supplied. All the chemicals were of food grade.
  • the molasses were beet molasses from De Danske Sukkerfabrikker.
  • Contraspum 210 (Zschimmer & Schwartz) was employed as the foam-suppressing agent, and sulfuric acid was employed as the pH regulating agent.
  • Yeast cells of strain ATCC 24261 were propagated by being transferred from a slant to a test tube with a diameter of 2 cm containing 5 ml of YM medium in which the cells were cultured for 4 days on a shake board under sufficient aeration at a temperature of 20-22°C, after which the culture was transferred to 2 I Erlenmeyer flasks containing 1 I of YM medium. After incubation for 3 days on a shake board and under sufficient aeration at a temperature of 20-22°C, 1 I of the culture was transferred to a 100 I fermenter containing 30 I of start wort. The culture was subjected to batch growth at 20-22°C until a yeast dry matter content of 1 g/l was obtained.
  • the nutrient supply was started and the fed-batch fermentation was performed at 20-22°C.
  • 30 I of the culture were transferred under sterile conditions by means of a peristaltic pump to the 4 m 3 fermenter which contained 2000 I of start wort.
  • the culture was subjected to batch growth at 20-22°C until a yeast dry matter content of 1 g/l in the culture was obtained.
  • the molasses supply was started and continued for 38 hours after which the molasses reservoir was depleted.
  • the chemicals were supplied proportionally with the molasses during the first 24 hours.
  • the fed-batch fermentation was performed at a temperature of 20-22°C.
  • the amount of molasses in the molasses reservoir was adjusted so that a yeast dry matter content of not more than about 4% in the fermented wort would be obtained.
  • the aeration of the fermented wort was continued for 16 hours at 20-22°C without any nutrient supply.
  • the composition of the yeast cells as well as the total pigment content and the astaxanthin content were measured at time 0, i.e. just before the nutrient supply to the 4 m 3 fermenter was started, after 38 hours when the fermentation and growth had terminated, and after 16 hours' aeration of the fermented wort.
  • the total pigment content and the astaxanthin content were determined as described in Example 2, and the composition of the yeast cells was determined by conventional techniques.
  • the total content of nitrogen was determined by Kjeldahl analysis
  • the trehalose content was determined as described in Journ. Am. Chem. Soc. 72 , 1950, p. 2059
  • the phosphoric acid content was determined as described in Water and Waste-water , American Public Health Association, Inc., p.
  • the total pigment and astaxanthin content in ⁇ g/ml has been calculated from the analyzed yeast dry matter content and ⁇ g/g-values of total pigment and astaxanthin.
  • the pigment and astaxanthin content of CBS 215-88 and the wildtype strains CBS 5905 and ATCC 24261 were determined.
  • yeast cells were inoculated in YM-medium and incubated for 2 days at 20-22 °C. 1 ml of the culture was inoculated in 50 ml of YM-medium, contained in 250 ml shake flasks with 4 baffles. The culture was subjected to growth on a shake board with orbital shaking at 150 rpm for 5 days at 20-22°C.
  • sucrose solution (0.30 g/l)
  • the addition rate was 2.3 l/hour.
  • Aeration was incereased to 8.4 m 3 /minute and the pH-controller started (set point 4.0).
  • the sucrose concentration in the medium was decreased to about 1 g/l after 28 hours, the sucrose supply was increased to 7.3 l/hour and kept at this rate for 24 hours. Thereafter sucrose supply was terminated and the aeration rate was decreased to 4.2 m 3 /minute and continued for 72 hours.
  • the total pigment and astaxanthin were determined during the fed-batch fermentation, giving the values stated in Table 7.
  • the yeast cells were separated from the medium by means of centrifugation in a De Laval OA5M centrifuge and washed with water twice.
  • the yeast was separated from the yeast cream by means of filtration in a FILTROX-filter, type VARIOX 40/40 cm and the filter cake with 26.3% dry matter was extruded through a 1 mm sieve in a lab fluid bed dryer (GLATT, Haltingen-Binzen Bd.) and dried at 30 °C for 90 minutes.
  • the dried yeast (91.6% of dry matter) contained 1360 ⁇ g total pigment/g yeast dry matter and 1080 ⁇ g astaxanthin/g yeast dry matter
  • Yeast cells obtained by the method of Example 3 were isolated from the fermented wort by centrifugation in a De Laval OA5M centrifuge. The cells were washed twice with water and a yeast cream with 13% of yeast dry matter was obtained. The pH of the yeast cream was adjusted to 4.0 by addition of sulphuric acid, and sodium benzoate was added to a concentration of 0.2% (w/v) in the yeast cream. During the treatment of the isolated yeast cells, these were under a nitrogen cover so as to prevent substantial oxidation of the astaxanthin of the yeast cells, and the temperature was kept at about 10 °C.
  • the yeast cream was subjected to three passages through a system consisting of an APV-Gaulin MC4 homogenizer provided with a cell rupture valve and a heat exchanger where the yeast cream was subjected to disintegration at a pressure of 700 bar, whereby the temperature increased by 10-15°C and subsequent cooling in the heat exchanger so as to obtain a temperature of 15°C.
  • the yeast cream was circulated in the system at a rate of 250 l/h.
  • the astaxanthin content in the disintegrated cells was determined as follows: 0.5 ml of homogenized yeast cream was weighed out and transferred to a Sarstedt tube and shaken with 5 ml of acetone. The sample was centrifugated, transferred to a 10 ml graduated cylinder, and washed 3 times with acetone with intervening centrifugations and quantitative transfers. The total pigment content was determined by method 1 and astaxanthin content was determined by HPLC-method 1, and the content was related to the total dry matter content in the sample which was determined by the method explained in Materials and Methods above.
  • the degree of disintegration in the present Example was determined to be more than 90% of the total cells.
  • the yeast cell homogenate in admixture with sodium caseinate was then subjected to spray drying in a spray tower of the type Anhydro in which the inlet temperature was 180°C.
  • the yeast cell mass was atomized by use of a spray wheel and the temperature of the air let out of the spraytower was of a temperature of about 90°C.
  • the resulting yeast powder was recovered by use of a cyclone.
  • the water content in the yeast powder was less than 10% by weight.
  • the yeast cells were extracted with 5 x 100 ml of glacial acetic acid at a temperature of 75 °C, and the amount of astaxantin in each of the extracts as well as in the extracted yeast cell material (including about 100 ml of glacial acetic acid remaining in the column) was determined.
  • the extracted yeast cell material had been evaporated to dryness (resulting in 16.16 g of material) before the astaxanthin determination was carried out.
  • Table 8 TABLE 8 Total astaxanthin content in yeast cell prior to extraction 20 g x 523 ⁇ g/g 10460 ⁇ g Astaxanthin content in 1. extract 100 ml x 55.7 ⁇ g/ml 5570 ⁇ g 2.
  • Phaffia rhodozyma yeast cells which had been dried in a fluid bed and which was found to contain 336 ⁇ g of astaxanthin/g of yeast dry matter, was suspended in soy bean oil in a concentration of 40% (w/w). The suspension was pumped to a ball mill (CoBall® - Mill, type MSZ-12) containing zirkonium balls (0.1-1.5 mm) and having a bead-filling of 70-75%. The bead of the rotor was 13 m/sec. Samples were taken after each run, and the astaxanthin content of the samples was analyzed on HPLC. The temperature in the ball mill was kept at 40-50 ° C.
  • Fish feed of varying astaxanthin contents were prepared.
  • the fish feed was made from the commercial fish feed Ecoline 16 from Dansk ⁇ rredfoder, Brande, Denmark, which is a mixture of fish meal, soy meal, fish oil, extruded wheat, lecitin and vitamins in the form of a premix.
  • Various amounts of astaxanthin were added to this feed.
  • the astaxanthin was obtained from P. rhodozyma yeast cells which had been grown in the same manner as described in Example 3 and which had been spray dried.
  • the spray dried yeast cells were prepared from 28 kg homogenized yeast cream which had been mixed with 0.475 kg of sodium caseinate dissolved in 2.7 kg water at about 50 °C.
  • GRINDTEK MOR 50 containing 2 g of ascorbyl palmitate and 1 g of tocopherols from soy beans was emulated in the sodium caseinate solution.
  • the sodium caseinate solution (containing antioxidants) was mixed with the homogenized yeast cream and the mixture was spray dried as described in Example 8.
  • the spray dried product (92.6% dry matter) contained about 674 ⁇ g of astaxanthin/g of yeast dry matter.
  • the spray dried product was added to the commercial fish feed so as to obtain the varying concentrations of astaxanthin in the fish feed (feed A-D) which appear from table 10 below.
  • feed E A fish feed containing synthetic astaxanthin was employed as a control.
  • the feed E contained synthetic astaxanthin in an amount corresponding to 40 ppm.
  • the feeds A-E had the following composition: TABLE 10 Fish feed A B C D E Astaxanthin ⁇ g/g feed 4.4 12.8 20.4 39.2 - Synthetic astaxanthin - - - - 40 Dry matter % 91.94 91.49 91.56 91.88 88.81 Ash % 9.12 9.00 8.79 8.45 7.03 cellulose % 1.46 1.45 1.60 2.05 1.71 Protein % 43.62 43.20 43.86 43.81 43.15 Fat % 17.59 17.21 18.62 20.00 21.19 Phosphor g/kg 11.58 10.89 11.25 10.80 9.96 Nitrogen-free extract % 20.15 20.53 18.69 17.57 15.73
  • the equipment used is equipment conventionally used in laboratory experiments.
  • a rainbow trout without skin was cut into pieces and 15 g of flesh were weighed out in a centrifugal tube (100 ml). 15 ml of tetrahydrofurane were added as extraction agent. The flesh was further divided in an ULTRATURAX mixer and subsequently centrifugated. The tetrahydrofurane extract was transferred to a 50 ml measuring flask. The remanence was washed with 10 ml of tetrahydrofurane for 2-3 minutes on a sonication bath and centrifugated, and the tetrahydrofurane phase was transferred to the measuring flask to which additional tetrahydrofurane was added up to 50 ml.
  • the colour of the fish flesh was determined by the L*a*b*-colour determination method by use of a Minolta Chroma Meter II.
  • the L*-value designates the light component
  • the a*-value designates the green/red component (the negative values designating the green component and the positive values designating the red component)
  • the b*-value designates the blue/yellow component of the colour. Only the a*-value is stated in Table 11.
  • the fish were also subjected to visual examination and were generally found to be of an attractive red colour. After 43 days of feeding, substantially no difference was observed in the pigmentation of fish fed with feed D and E (containing about 40 ppm astaxanthin produced according to the present invention and 40 ppm synthetic astaxanthin, respectively). After 72 days of feeding, substantially no difference was observed in the pigmentation of fish fed with feed C, D and E (containing about 20 ppm astaxanthin produced according to the present invention, 40 ppm astaxanthin produced according to the present invention, and 40 ppm synthetic astaxanthin, respectively).
  • a fish paté (salmon-like) in which astaxanthin is used to impart the red colour can be made according to the following recipe: Cod scraps 71 % Oil 3% Rusk 4% Grindsted Protein 177*) 1% Starch 1% Astaxanthin 0.001 % Water, preservatives and spices up to 100% *) Grindsted Protein 177 is a blend of 75% of Grindsted Protein 100 and 25% of sodium alginate.
  • the astaxanthin was dispersed in the oil phase.
  • the Grindsted Protein 177, starch and other dry ingredients were mixed, and the fish were added to a colloid mill. Then, the oil phase, the dry ingredients and water were added, and processing was continued in the colloid mill for about 10 minutes.
  • the paté was filled into tins and subjected to heat treatment.
  • a red dressing with an attractive red colour can be prepared by conventional methods from the following ingredients: Oil 30.0% Tarragon vinegar 12.3% Tomato paste 8.0% Mayodan DC *) 0.3% Sugar 8.0% Salt 0.8% Astaxanthin 0.01-0.5% Water, preservatives and spices up to 100% *) Mayodan DC® is a stabilizer blend from Grindsted Products A/S.

Claims (14)

  1. Phaffia rhodozvma Hefezelle, welche eine Hefezelle ist, die zu dem Hefestamm, der unter der Hinterlegungsnummer 225-87 CBS hinterlegt ist, oder dem Hefestamm, der unter der Hinterlegungsnummer 215-88 CBS hinterlegt ist, gehört, oder eine Mutante oder ein Derivat davon, oder eine Mutante oder ein Derivat des Hefestammes, der unter der Hinterlegungsnummer 224-87 CBS hinterlegt ist, welche bzw. welches ihre bzw. seine Fähigkeit zur Produktion von Astaxanthin beibehalten hat, und, wenn sie bzw. es unter Bedingungen, welche eine Sauerstofftransferrate von mindestens 30 mmol/l/h umfassen, auf Difco YM Medium bei 20 - 22°C fünf Tage lang in 500 ml Schüttelflaschen mit zwei Schikanen, welche 50 ml Medium enthalten und bei 150 U/min kreisförmig geschüttelt werden, kultiviert wird, wobei die Impfkultur 100 µl einer 4 Tage alten YM-Kultur ist, Astaxanthin in einer Menge von mindestens 600 µg pro g Hefetrockenmasse produziert, bestimmt durch HPLC-Analyse eines Methanolextraktes der Hefe, welcher hergestellt wird, indem eine Suspension von 0,2 g Hefetrockenmasse in 20 ml Methanol 5 x 1 Minute lang in Intervallen von einer halben Minute aufgebrochen wird, wobei das Aufbrechen bei einer Temperatur von maximal 20°C in einer Glaskugelmühle, welche 15 g Glaskugeln mit einem Durchmesser von 0,4 mm enthält, durchgeführt wird, wobei die Glaskugelmühle mit einem Kühlmantel mit Eiswasser ausgestattet ist, wobei reines Astaxanthin als Standard verwendet wird.
  2. Hefezelle nach Anspruch 1, welche, wenn sie unter den in Anspruch 1 angegebenen Bedingungen kultiviert wird, Astaxanthin in einer Menge von mindestens 700 µg pro g Hefetrockenmasse, vorzugsweise mindestens 1000 µg pro g Hefetrockenmasse, produziert, bestimmt durch das in Anspruch 1 angegebene Verfahren.
  3. Verfahren zum Produzieren von astaxanthinhaltigen Phaffia rhodozyma Hefezellen oder Zellteilen oder Astaxanthin, welches das Kultivieren von Astaxanthin produzierenden Phaffia rhodozyma Hefezellen wie in einem der Ansprüche 1 oder 2 beansprucht unter aeroben Bedingungen in einem Medium, das Kohlenhydratquellen, assimilierbare Stickstoff- und Phosphorquellen, Mikronährstoffe und Biotin oder Desthiobiotin enthält, bei einer Temperatur im Bereich von 15 - 26°C, um eine Biomasse zu erhalten, die Astaxanthin in einer Menge von mindestens 600 µg pro g Hefetrockenmasse, bestimmt durch das in Anspruch 1 angegebene Verfahren, enthält, und wahlweise das Durchführen von einem oder mehreren der folgenden Schritte in willkürlicher Reihenfolge umfasst:
    - Ernten der Zellen aus der Kultur, um eine Hefecreme zu erhalten,
    - Öffnen der Zellen, z.B. Aufbrechen der Zellwände mittels mechanischer, chemischer und/oder enzymatischer Behandlung und/oder Behandeln der Zellen durch Beschallung, Autolyse, Osmolyse und/oder Plasmolyse wahlweise mit Zugabe von geeigneten Mitteln wie Detergenzien, Säuren, Basen, Enzymen, autolysefördernden Substanzen, osmolytischen Mitteln wie Salzen und/oder plasmolytischen Mitteln,
    - Homogenisieren der Zellen, um ein Homogenisat zu erhalten,
    - Trocknen der Zellen, der Zellfragmente oder des Homogenisats, vorzugsweise bis zu einem Wassergehalt von maximal 12 Gew.-%, vorzugsweise maximal 10 Gew.-%,
    - Extrahieren von Astaxanthin aus den Zellen, den Zellfragmenten oder dem Homogenisat.
  4. Verfahren nach Anspruch 3, worin die Kultivierung als Fedbatch-Fermentation unter Bedingungen durchgeführt wird, wo im Wesentlichen kein Alkohol gebildet wird, und wahlweise wo die gesamte Konzentration von Glucose und Saccharose maximal 8 g/l, vorzugsweise 5 g/l und am meisten bevorzugt 1 g/l ist, vorzugsweise bei einer Temperatur von 20 - 22°C, die Fermentation oder ein Teil davon in einem Medium durchgeführt wird, welches Melasse und/oder Saccharose und Stickstoffquellen wie Diammoniumsulfat, Ammoniumphosphat, Ammoniumhydroxid oder Harnstoff, Phosphorquellen wie Ammoniumphosphat und Phosphorsäure und zugegebene Mikronährstoffe oder Mineralsalze wie Magnesiumsulfat, Zinksulfat und Biotin oder Desthiobiotin umfasst, wobei die Melasse wahlweise dem Medium getrennt von den anderen Komponenten zugeführt wird.
  5. Verfahren nach den Ansprüchen 3 oder 4, worin die Kultivierung eine Wachstumsphase unter Bedingungen, welche im Wesentlichen ausreichend im Hinblick auf im Wesentlichen alle Wachstumsbedingungen sind, und eine nachfolgende wachstumsbeschränkte Phase unter Bedingungen, wo das Wachstumsmedium unter fortgesetzter Belüftung an mindestens einem Wachstumsfaktor Mangel hat, so dass die Produktion von Astaxanthin während der nachfolgenden Phase gefördert wird, umfasst.
  6. Verfahren nach Anspruch 5, worin die nachfolgende wachstumsbeschränkte Phase eine Dauer von mindestens etwa 16 Stunden, wie 16 - 24 Stunden hat, die nachfolgende wachstumsbeschränkte Phase vorzugsweise so eingerichtet ist, dass die Astaxanthinproduktion auf mindestens das 1,2fache der Produktion, die ohne die nachfolgende Phase erhalten wird, vorzugsweise auf mindestens das 1,3fache, wie etwa das 1,4fache und noch mehr bevorzugt das 1,5fache der Produktion, die ohne die nachfolgende Phase erhalten wird, gesteigert wird, wobei die nachfolgende wachstumsbeschränkte Phase vorzugsweise im Wesentlichen ohne jede Zugabe eines Nährstoffes oder Mikronährstoffes zu dem Medium durchgeführt wird.
  7. Verfahren nach einem der Ansprüche 3 - 6, worin die Konzentration von Astaxanthin in der Biomasse mindestens 600 µg pro g Hefetrockenmasse, vorzugsweise mindestens 700 µg pro g Hefetrockenmasse, bestimmt durch das in Anspruch 1 angegebene Verfahren, beträgt.
  8. Verfahren nach Anspruch 7, worin die erhaltene Konzentration von Astaxanthin in der Biomasse mindestens 600, vorzugsweise mindestens 800, mehr bevorzugt mindestens 1000 µg pro g Hefetrockenmasse, ist, wobei die Konzentration durch das in Anspruch 1 angegebene analytische Verfahren bestimmt wird.
  9. Verfahren nach einem der Ansprüche 4 - 8, worin die Hefezellen, im Anschluss an die Kultivierung und die wahlfreie nachfolgende wachstumsbeschränkte Phase, einer oder mehreren der folgenden Behandlungen unterworfen werden:
    - Aufbrechen der Zellen durch Aussetzen der Zellen einem erhöhten Druck und dann Abfallenlassen des Druckes und anschließendes Unterwerfen der aufgebrochenen Zellen einer Ultrafiltration oder Verdampfung, um die aufgebrochenen Hefezellen zu konzentrieren,
    - Aufbrechen der Zellen durch Aussetzen der Zellen einem erhöhten Druck und dann Abfallenlassen des Druckes und anschließendes Sprühtrocknen oder Trommeltrocknen der aufgebrochenen Zellen,
    - Filtration, um einen Filterkuchen zu erhalten, der dann extrudiert wird, wonach das Extrudat getrocknet wird, z.B. in einem Fließbett oder durch Trocknen in Schalen,
    - Mischen von Trockenmaterial aus ganzen Zellen, welches in einem Fließbett oder durch Trocknen in Schalen getrocknet wurde, mit einer öligen Phase wie einem essbaren Öl oder Fett und Mahlen des Gemisches in einer Mühle wie einer Kugelmühle, um die Zellen aufzubrechen und Astaxanthin in die ölige Phase freizusetzen,
    - Extrahieren von aufgebrochenen Zellen, die vorzugsweise homogenisiert sind, mit organischen Lösungsmitteln wie Petrolether, Aceton, oder einem Alkohol wie Methanol, Ethanol oder Isopropanol, um in dem organischen Lösungsmittel gelöstes Astaxanthin zu erhalten, und dann wahlweise Entfernen des Lösungsmittels wie etwa durch Verdampfung,
    - Extrahieren von ganzen Zellen mit einem Lösungsmittel, welches Eisessig umfasst, um in dem eisessighaltigen Lösungsmittel enthaltenes Astaxanthin zu erhalten,
    - Superkritische Extraktion von aufgebrochenen oder ganzen feuchten oder trockenen Zellen mit Kohlendioxid, wahlweise in Kombination mit organischen Lösungsmitteln, z.B. von der oben erwähnten Art.
  10. Verfahren nach Anspruch 9, worin die Behandlungen unter sauerstoffbeschränkten Bedingungen wie in einer Inertatmosphäre, z.B. der Inertatmosphäre, die mittels Wasserdampf und/oder mittels Stickstoff und/oder Kohlendioxid hergestellt wird, durchgeführt werden.
  11. Verfahren nach Anspruch 9 oder 10, worin die Extraktion der ganzen Hefezellen und des eisessighaltigen Lösungsmittels bei einer Temperatur oberhalb des Gefrierpunkts des Lösungsmittels, z.B. im Bereich von 20 - 100°C, vorzugsweise im Bereich von 20 - 80°C und noch mehr bevorzugt im Bereich von 20 - 60°C durchgeführt wird.
  12. Tierfutter umfassend Phaffia rhodozvma Hefezellen nach Anspruch 1 oder Hefezellteile, welche Astaxanthin in einer Menge von mindestens 600 µg pro g Hefetrockenmasse enthalten, bestimmt durch das in Anspruch 1 angegebene Verfahren, in Kombination mit andern Futtermittelbestandteilen, vorzugsweise Tierfutter, worin die astaxanthinhaltigen Hefezellen oder Hefezellteile maximal 10 Gew.-% der Trockenmasse der gesamten Tierfutterzusammensetzung, vorzugsweise maximal 5 % und noch mehr bevorzugt maximal 3 % ausmachen, wobei die anderen Bestandteile vorzugsweise ausgewählt sind aus Protein- und Kohlenhydratquellen wie Fischmehl, Molke, Blutmehl, Pflanzenmehle, Fetten wie Fischöl und Pflanzenöle, Vitaminen und Mineralstoffen.
  13. Tierfutter nach Anspruch 12, worin die astaxanthinhaltigen Hefezellen oder Hefezellteile Hefezellen nach Anspruch 1 oder Teile davon oder Hefezellen oder Hefezellteile, die nach dem Verfahren nach einem der Ansprüche 3 - 11 produziert werden, sind.
  14. Verfahren zum Füttern von Tieren, um eine rötliche Pigmentierung ihres Fleisches und/oder von Produkten, die von den Tieren erzeugt werden, zu erhalten, welches das Verabreichen eines Futters an die Tiere umfasst, welches Phaffia rhodozyma Hefezellen nach Anspruch 1 oder 2 oder Zellteile enthält, die Astaxanthin in einer Menge von mindestens 600 µg pro g Hefetrockenmasse enthalten, bestimmt nach dem in Anspruch 1 angegebenen Verfahren, wobei die Tiere vorzugsweise Fische, insbesondere Lachs oder Lachsforelle (sea trout), Kühe zum Pigmentieren ihrer Butter oder Geflügel zum Pigmentieren ihrer Eidotter sind.
EP88903778A 1987-04-15 1988-04-15 Astaxantin liefernde hefezellen, verfahren zur herstellung Expired - Lifetime EP0367765B2 (de)

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EP0367765A1 (de) 1990-05-16
US5972642A (en) 1999-10-26
JPH0714340B2 (ja) 1995-02-22
DE3883539D1 (de) 1993-09-30
WO1988008025A1 (en) 1988-10-20
NO885560L (no) 1989-02-14
DE3883539T2 (de) 1994-03-17
KR890700658A (ko) 1989-04-26
JPH1169969A (ja) 1999-03-16
IS1580B (is) 1996-03-01
ATE93537T1 (de) 1993-09-15
NO885560D0 (no) 1988-12-14
DE367765T1 (de) 1990-08-16
DE3883539T3 (de) 2005-02-03
KR960014619B1 (ko) 1996-10-19
IE881151L (en) 1988-10-15
DK199887D0 (da) 1987-04-15
EP0367765B1 (de) 1993-08-25
FI894888A0 (fi) 1989-10-16
CA1334512C (en) 1995-02-21
AU620034B2 (en) 1992-02-13
JPH02504101A (ja) 1990-11-29
AU1688988A (en) 1988-11-04
NO305762B1 (no) 1999-07-19
IS3334A7 (is) 1988-10-16
HK1005464A1 (en) 1999-01-08
IE60606B1 (en) 1994-07-27

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